Dehydrogenation of alcohols to ketones

ABSTRACT

A Group VIII metal containing pyrolyzed polyacrylonitrile polymer catalyst and hydrocarbon conversion process for the dehydrogenation of alcohols to ketones particularly isopropyl alcohol to acetone and the hydrogenation of nitro compounds to amines, particularly 2-nitropropane to isopropyl amine by the use of said catalyst.

United States Patent Schwager et al.

[15] 3,671,591 51 June 20, 1972 DEHYDROGENATION OF ALCOHOLS TO KETONES Inventors: Irving Schwager, Hopewell Junction;

Robert J. Leak, Wappingers Falls; Edward L. Cole, Fishkill, all of NY.

Assignee: Texaco Inc., New York, NY.

Filed: July 3, 1969 Appl. No.: 839,082

US. Cl. 260/596, 252/430, 260/563 D, 260/580, 260/583 M, 260/583 P, 260/586 B,

Int. Cl ..C07c 45/16, C07c 85/10 Field of Search ..260/596 [56] References Cited UNITED STATES PATENTS 3,173,933 3/1965 Hay ..260/596 X Primary Examiner.loseph Rebold Assistant E.\'aminer-Richard L. Raymond A!!0rneyl(. E. Kavanagh and Thomas H. Whaley [5 7] ABSTRACT 7 Claims, No Drawings DEI'IYDROGENATION OF ALCOHOLS TO KETONES This invention relates to a new Group VIII metal containing pyrolyzed polyacrylonitrile polymer catalyst and to a hydrocarbon conversion process utilizing said catalyst for the dehydrogenation of alcohols to ketones and the hydrogenation of nitro compounds to amines.

In the dehydrogenation of alcohols to ketones many catalysts have been used such as'copper chromite to effect dehydrogenation. In addition, a dehydrogenation catalyst of the prior art such as copper chromite has in addition been used for the hydrogenation of nitro compounds to amines. A

particular problem associated with the use of a catalyst for both a dehydrogenation and hydrogenation process is the necessity for selective conversion to the desired product without the formation to any substantial degree of undesired side reaction products, while maintaining a high percent conversion to the desired product. Thus, the dehydrogenation of an alcohol such as isopropyl alcohol to acetone can result in the formation of propylene and other light gases as side reaction products whereas the hydrogenation of a nitro compound such as 2-nitropropane to isopropylamine can result in the formation of diisopropyl amine and isopropyl alcohol. As is apparent from the foregoing, there exists the problem of selective conversion of the starting reactant to the desired product at high conversions. The formation of undesired side reaction products decreases the yield of product and in addition contaminates the desired product necessitating additional treating steps for the removal of contaminants. As is apparent from the foregoing, there is incentive to discover processes whereby a catalyst can be utilized for both the dehydrogenation of alcohols to ketones and the hydrogenation of nitro compounds to amines in good yields while minimizing any side reactions and the formations of undesired products.

It is therefore an object of this invention to dehydrogenate alcohols to ketones and hydrogenate nitro compounds to amines, at high yields while minimizing the formation of undesired products.

It has now been found that organic secondary alcohols can be dehydrogenated to organic ketones and organic nitro compounds hydrogenated to organic primary amines utilizing a novel catalyst by a process which comprises contacting an organic secondary alcohol or an organic nitro compound under dehydrogenation and hydrogenation conditions respectively with a catalytic amount of a Group VIII metal containing pyrolyzed polyacrylonitrile polymer and recovering an organic ketone and organic primary amine respectively. Thus it has been found that when an organic secondary alcohol is contacted with a catalytic amount of a Group VIII containing pyrolyzed polyacrylonitrile polymer, hereinafter referred to as catalyst, a high yield of an organic ketone is produced while minimizing the formation to any substantial extent of secondary reactions and secondary products such as light gases. More particularly, it has been found that when isopropyl alcohol is contacted with a catalytic amount of catalyst, conversions often above 90 percent mole percent to acetone with minimum formations of propylene and other light gases, generally below 10 mole percent and more often below 5 mole percent are achieved. These results are in sharp contrast to a platinum on an activated carbon catalyst wherein only 4 mole percent acetone is formed with the formation of 96 mole percent propylene. In addition, the above catalyst under hydrogenation condition catalytically converts organic nitro compounds to organic amines at high yields while minimizing side reactions and formation of undesired products. More particularly, the hydrogenation of 2-nitropropane to isopropyl amine utilizing the above catalyst can produce yields above 90 mole percent often above 95 mole percent with minimum formation of undesired products such as diisopropyl amine and isopropyl alcohol generally below mole percent. These results are in sharp contrast to complete inactivity of platinum on silica gel.

In general the dehydrogenation process of this invention is carried out by contacting the organic secondary alcohol with a catalytic amount of catalyst under dehydrogenation conditions of temperature and pressure sufficient to produce an organic ketone, whereas the hydrogenation process is carried out by contacting an organic nitro compound with a catalytic amount of catalyst under hydrogenation conditions of temperature, pressure, and hydrogen concentrations sufficient to produce an organic primary amine. The term catalytic amount for the dehydrogenation process is used herein to mean that concentration by weight of catalyst which during dehydrogenation produces a yield of organic ketone in excess of other side reaction products, preferably at a conversion of at least mole percent. In general, a concentration of catalyst of from about I to about 20 weight percent more preferably from about 5 to about 10 weight percent based upon the weight of the starting organic secondary alcohol is utilized during the hydrogenation process. The product, that is the organic ketone, is then recovered by conventional means.

In carrying out the hydrogenation process, a catalyst concentration is utilized which produces a yield of organic mono amine greater than production of side reaction products, preferably at a conversion of at least 90 mole percent. In general, a concentration of catalyst of from about I to about 20 weight percent, more preferably from about 5 to about 10 weight percent based upon the weight of the organic nitro component is utilized during the hydrogenation process. The organic primary amine is then recovered by conventional means.

The conditions for dehydrogenation can be varied over a wide range as to liquid hourly space velocity (LHSV, volume of organic secondary alcohol to volume of catalyst per hour), temperature, pressure, and the concentration of catalyst. These conditions are adjusted in order to produce a dehydrogenation step wherein the catalyst is present in a concentration sufficient to effect conversion of the organic secondary alcohol to the organic ketone, and are adjusted in order to maximize such yield while minimizing the formation of side reaction products.

The organic secondary alcohol is dehydrogenated in general at a temperature of from about 250 F. to about 700 F., preferably from about 350 F. to about 500 F. pressures of from about 0.1 to about I00 psig., preferably from about 0.5

to about 15 psig. and liquid hourly space velocities of from about 0.1 to about 5, preferably from about 0.2 to about 1 (volumes of organic secondary alcohol per volume of catalyst per hour).

The conditions for hydrogenation can be varied over a wide range as to liquid hourly space velocity (LHSV, volume of feed to volume of catalyst per hour), hydrogen gas rate (volume of hydrogen to volume of organic nitro compound, s.c.f./bbl.), temperature, pressure, and the concentration of catalyst. These conditions are adjusted in order to produce a hydrogenation step wherein the hydrogen and catalyst are present in a concentration sufficient to effect production of organic amine and are adjusted in order to maximize the yield of organic amine while minimizing the side reaction products.

The organic nitro compound is contacted with hydrogen in general at a temperature of from about 200 F. to about 500 F., preferably from about 250 F. to about 350 F.; pressures of from about 5 to about 1,000 psig., preferably from about 15 to about 500 psig; liquid hourly space velocities of from about 0.1 to about 5, preferably from about 0.2 to about 1 volumes of feed per volume of catalyst per hour; and hydrogen rates of from about 500 to about 2,500, preferably from about 1000 to about 2,000 standard cubic feet.(s.c.f./bbl.) of feed.

As stated above the process of this invention utilizes one or more novel Group VIII metal containing pyrolyzed polyacrylonitrile polymers. In general tee catalyst is prepared by the process which comprises pyrolyzing a polyacrylonitrile polymer under pyrolysis conditions of temperature and pressure, contacting the pyrolyzed polymer from the preceding step with a Group VIII metal and recovering a Group VIII metal containing pyrolyzed polyacrylonitrile polymer, containing from 0.2 to about 50 weight percent Group VIII metal.

By the use of the term polyacrylonitrile polymers ismeant, a polyacrylonitrile polymer which comprises at least about 80 weight percent of the polymerized monomer units being derived from acrylonitrile more preferably 90 weight percent. The polyacrylonitrile polymer is then subjected to conditions of pyrolysis. As stated above, it is preferred that the starting polyacrylonitrile polymer have at least 80 weight percent of the polymerized monomer units being derived from acrylonitrile. Thus the remaining 20 percent by weight can be other monomers which polymerize with acrylonitrile. In a still more preferred sense it is preferred that the polyacrylonitrile polymer be derived substantially from acrylonitrile, that is at least 95 weight percent being derived from acrylonitrile. The polyacrylonitrile polymers are for the most part amorphous solids or crystallinesolids. It will beunderstood that for the purposes of this specification that the term polymer is used in a generic sense to include homopolymers, copolymers, terpolymers or other. inter polymers which have molecular weights of at least about 25 ,000, more preferably from about 25,000 to about 1,300,000.

Acrylonitrile is usually polymerized by the free radical polymerization technique (also known as the addition polymerization technique). Such technique consists of contacting the monomers with polymerization initiator either in the absence or presence of a diluent at a temperature usually between and 200 C. The polymerization initiator is a substance capable of liberating a free radical under the conditions of polymerization, e.g., benzoyl peroxide, tert-butyl hydroperoxide, cumyl peroxide, potassium persulfate, acetyl peroxide, hydrogen peroxide, azobisisobutyronitrile, or perbenzoic acidQFor reasons of economy, benzoyl peroxide or azobisisobutyronitrile are most commonly used.

Acrylonitrile may also be polymerized or copolymerized using an anionic initiatorsuch as naphthylsodium or butyllithiurn in tetrahydrofuran solution or sodium metal in liquid ammonia solution.

The polymerization of acrylonitrile may also be effected by other polymerization techniques such as by the use of Ziegler type catalysts, gamma ray irradiation, or thermal techniques.

Thediluent for the polymerization mixture may be either an inert solvent such as benzene, toluene, xylene, cyclohexane, n-

. hexane, naphtha, tetrahydrofuran, white oil, or dodecane; or a non-solvent such as. water or liquid ammonia; Thus, the polymerization can be carried out in bulk, solution, emulsion, or suspension.

The temperature for the polymerization depends on the catalyst system employed and to some extent upon the nature of the monomers to be polymerized. Thus, the copolymerization of acrylonitrile with an acrylamide may be catalyzed by an anionic initiator at temperatures from about l00 to 50 C., preferably at 70 to 0 C. On the other hand, the optimum temperature for effecting the free radical catalyzed homopolymerization of acrylonitrile is usually from 0 to 100 C., preferably 30 to 80 C. Similarly, the optimum temperatures for effecting the free radical catalyzed interpolymerization of acrylonitrile with one or more polymerizable comonomers will vary according to .the reactivity of these monomers. In most instances such temperatures likewise are within the range from about 0 to 100 C.

A large variety of comonomers can be used to form interpolymers with the acrylamides of this invention. For the most part, the comonomers are polymerizable vinyl monomers. They include, for example: (1) esters of unsaturated alcohols, (2) esters of unsaturated acids, (3) vinyl cyclic compounds, (4) unsaturated ethers, (5) unsaturated ketones, (6) unsaturated amides, (7) unsaturated aliphatic hydrocarbons, (8) vinyl halides, (9) esters of unsaturated polyhydric alcohols (e.g., butenediol), (10) unsaturated acids, (11) unsaturated acid anhydrides, (12) unsaturated acid chlorides, and (13) unsaturated nitriles other than acrylonitrile.

Specific illustrations of such compounds are:

l. Esters of unsaturated alcohols: Allyl, methallyl, crotyl, lchlorallyl, 2-chloroallyl, cinnamyl, vinyl, methyl-vinyl, 1-

phenallyl, butenyl, etc., esters of (a) saturated acids such as for instance, acetic, propionic, butyric, valeric, caproic, stearic, etc.; (b) unsaturated acids such as acrylic, alpha-substituted acrylic. (including alkacrylic, e.g., methacrylic, ethylacrylic, propylacrylic, etc.), crotonic, oleic, linoleic, linolenic, etc., (c) polybasic acids such as oxalic, malonic, succinic, glutaric, adipic, pimelic, suberic, azelaic, sebacic, etc., (d) unsaturated polybasic acids such as maleic, fumaric, citraconic, mesaconic, itaconic, methylenemalonic,

1 acetylenedicarboxylic aconitic, etc., (e) aromatic acids, e.g.,

benzoic, phenylacetic, phthalic, terephthalic, benzolyphthalic,

etc. 1

2. The esters of saturated alcohols such as methyl, ethyl, propyl, isopropyl, butyl, isobutyl, sec-butyl, tert-butyl, 2-ethylhexyl, cyclohexyl, benzyl, etc., with unsaturated aliphatic monobasic and polybasic acids, examples of which are illustrated above.

3. Esters of unsaturated polyhydric alcohols, e.g., butenediol, etc., with saturated and unsaturated aliphatic and aromatic, monobasic and polybasic acids, illustrative examples of which appear above.

4. Vinyl cyclic compounds including (a) monovinyl aro matic hydrocarbons, e.g., styrene, o-, m-, p-chlorostyrenes, bromostyrenes, -fluorostyrenes, -methylstyrenes, -ethylstyrenes, -cyanostyrenes, do-, tri-, and tetra-, etc., chlorostyrenes, -bromostyrenes, -flurostyrenes, -methylstyrenes, -ethylstyrenes, -cyanostyrenes, vinylcyclohexane, vinylfuran, vinylpyridine, vinylbenzofuran, divinybenzene, trivinylbenzene, allybenzene, N-vinylcarbazole, N-vinylpyrrolidone, N-vinyloxazolidone, etc.

5. Unsaturated ethers such as, e.g., methyl vinyl ether, ethyl vinyl ether, cyclohexyl vinyl ether; octyl vinyl ether, diallylether, allyl ethyl ether, etc.

6. Unsaturated ketones, e.g., methyl vinyl ketone, ethyl vinyl ketone, etc.

7. Unsaturated amides, such as acrylamide, N-methylacrylamide, N-phenylacrylamide, N-allylacrylamide, N

methylolacrylarnide, N-allycaprolactam, etc.

8. Unsaturated aliphatic hydrocarbons, for instance, ethylene, propylene, butenes, butadiene, isoprene, 2-chlorobutadiene, alpha-olefins, etc.

9. Vinyl halides, e.g., vinyl fluoride, vinyl chloride, vinyl bromide, vinyl iodide, vinylidene chloride, vinylidene bromide, allyl chloride, allyl bromide, etc.

l0. Unsaturated acid anhydrides, e.g., maleic, citraconic, propylacrylic, etc., examples of which appear above.

11. Unsaturated acidanhydrides, e.g., maleic, citraconic, itaconic, cis-4-cyclohexene-l, 2-dicarboxylic, bicyclo (2.2.1) 5-heptene-2, 3-dicarboxylic, etc.

12. Unsaturated acid halides such as cinnamoyl, acrylyl, methacrylyl, crotonyl, oleyl, fumaryl, etc.

13. Unsaturated nitriles other than acrylonitrile, e.g., methacrylonitrile and other substituted acrylonitriles.

The solid polyacrylonitrile polymer is then subjected to a pyrolysis step. As stated above the pyrolysis of the polyacrylonitrile polymer is carried out in the presence of oxygen, preferably in the presence of air. In general the conditions as to time, temperature, pressure and oxygen concentration which are utilized are temperatures of from about 300 to about 500 F., more preferably from about 350 to about 450 F. pressures of from about 0.1 to about 2 atm., preferably of from about 0.5 to about 1 atrn. and a contact time in hours of from about 6 to about 96, more preferably from about 12 to about 48. It is preferred in preparing the pyrolyzed polymers 'to pelletize the solid polymer prior to pyrolysis. After the pyrolysis step either a tan to brown solid material, or a black solid carbonaceous material is generally recovered.

The polyacrylonitrile polymer in general is converted to the Group VIII metal containing pyrolyzed polyacrylonitrile polymer by contacting the pyrolyzed polyacrylonitrile polymer with an aqueous solution of a Group VIII metal salt or acid, preferably the Group VIII metal chloride or chloro acid such as chloroplatinic acid. The catalyst is then recovered by evaporating the aqueous solution of polymer and Group VIII metal salt or acid to remove water, thermally treating the polymer, preferably in an inert atmosphere, followed by hydrogen reduction at elevated temperatures. In general concentrations of Group VIH metal salt or acid based upon the weight of the polymer of from about 0.2 weight percent to about 50 weight percent are utilized in preparing the catalyst. In general temperatures of from about 400 F. to about 700 F., more preferably from about 550 F. to about 650 F. in an inert atmosphere are utilized for the thermal treatment step. In the hydrogen reduction step, temperatures of from about 500 F. to about 700 F. in a hydrogen atmosphere, preferably at pressures from about psig. to about 50 psig. and at hydrogen gas rates of from about 0.5 cu.ft./hr. to about 2.0 cu.ft./hr. are utilized. The preferred metal content of the catalyst is from about 0.2 weight percent to about 50 weight percent still more preferably from about 0.5 weight percent to about 5.0 weight percent based upon the weight of the catalyst. It is preferred that the catalyst contain platinum, palladium, or nickel as the Group VHI metal.

It is contemplated within the scope of this invention that both the dehydrogenation and hydrogenation process when practiced on a continuous basis can provide for recycle of non-converted organic secondary alcohols and organic nitro compounds respectively to the feed stock for reprocessing. In addition, it is contemplated within the scope of this invention that the hydrogenation and dehydrogenation process can be carried out in batch, continuousand semi-continuous cycles employing hydrogenation and dehydrogenation equipment such as heretofore have been employed for the preparation of organic ketones from organic secondary alcohols and organic primary amines from organic nitro compounds. In addition, a multi-stage mode of operation that is a repeating of the process several times can be utilized in practicing the process of this invention.

A wide variety of organic secondary alcohols can be utilized in the proccss of this invention as well as a wide variety of organic nitro compounds for conversion to primary amines.

Typical examples of starting reactants are organic secondary alcohols represented by the structure:

and organic nitro compounds represented by the structure:

R"'NO wherein R, R, and R are each a hydrocarbon radical and can be the same or different.

It is particularly preferred that such hydrocarbon radicals contain from one to about 30 carbon atoms, more preferably from one to about eight carbon atoms.

Typical examples of hydrocarbon radicals are alkyl radicals such as methyl, ethyl, isopropyl, butyl, t-butyl, 3-methyl-1- pentyl, and n-octyl, cycloalkyl radicals such as cyclopentyl, alkylated cycloalkyl radicals such as mono and polymethylcyclopentyl radicals, aryl and cycloalkyl substituted alkyl radicals such as phenyl and alkylphenyl substituted alkyl radicals examples of which are benzyl, methylbenzyl, caprylbenzyl, phenylethyl, phenylpropyl, naphthylmethyl, naphthylethyl, aryl radicals such as phenyl, and naphthyl, alkaryl radicals such as xylyl, alkylphenyl, and ethylphenyl.

Typical examples of organic secondary alcohols are isopropyl alcohol, secondary butyl alcohol, 2-octano1, 3-ethyl- 2-pentanol, 3-rnethoxy-2-propanol, 3-phenyl-2-propanol, 4- phenyl-Z-Pentanol.

Typical examples of organic nitro compounds which canbe converted to organic amines are l-nitropropane, 2- nitropropane, nitrobenzene, 1,1-dinitrodiphenyl, l-nitrooctane, l-nitrooctadecane, 1,-dinitrohexamethylene, 2- nitrooctane, and Z-nitrooctadecane.

The invention can be better appreciated by the following non-limiting examples:

EXAMPLE 1 To a three-neck l-liter flask equipped with stirrer ther mometer and reflux condenser is added under a nitrogen atmosphere 55 grams (1.0 mole) of acrylonitrile, 750 milliliters of water and 1.0 gram of azo-bis-isobutyronitrile. The mixture is heated with stirring to a temperature of 140 F. which is maintained for a period of 2 hours. After this period, 1 additional gram of azo-bis-isobutyronitrile is added and the mixture stirred at 140 F. for an additional two hours. The mixture is reduced to ambient temperature and a solid polymer is recovered by filtration. The polymer is washed with water, partially air dried and dried for 12 hours at 250 F. A white polymer 36 grams is recovered. The polymer (36 grams) is then pyrolyzed at 300 to 450 F. in an air stream over a period of 12 hours. A brown material (32 grams) is obtained which is then pelleted and calcined at 800 F. for a period of 30 minutes under a nitrogen atmosphere. A yield of 21 grams of black material is then recovered which has 67.2 weight percent carbon, 2.9 weight percent hydrogen, 18.1 percent nitrogen and a surface area of 2 meters per gram. The

pyrolyzed polyacrylonitrile polymer 10 grams) together with an aqueous solution (5.0 ml) containing 2.5 weight percent of chloroplatinic acid are added to a glass flask equipped with stirrer. The temperature is increased to 200 F. with stirring, and the temperature maintained for a period of 2 hours during which time the water evaporates from the mixture. After the water has evaporated from the mixture, the temperature is increased to 600 F. under a nitrogen atmosphere for a period of 3 hours. The temperature is reduced to ambient temperature and hydrogen at atmospheric pressure is passed through the catalyst mixture as the temperature is increased to 600 F. The temperature is maintained for a period of 2 hours after which the temperature is reduced to ambient temperature. A platinum containing pyrolyzed polyacrylonitrile polymer is recovered which has a platinum content of 0.5 weight percent.

EXAMPLE 2 Example 1 is repeated except 12 ml. of an aqueous nickel acetate solution containing 17.5 weight percent nickel acetate is utilized in place of the chloroplatinic acid solution. A nickel containing pyrolyzed polyacrylonitrile polymer is recovered which has a nickel content of 5.0 weight percent.

EXAMPLE 3 To a 3 neck 1 liter flask equipped with stirrer, thermometer, and reflux condenser is added in a nitrogen atmosphere 55 grams of acrylonitrile, 3.0 grams of methylmethacrylate, 750 milliliters of water and 1.0 grams of azobisisobutymonitrile. The mixture is heated with stirring to a temperature of F. which is maintained for a period of 2 hours. After this period 1 gram of azobisisobutyronitrile is added and the mixture stirred at 140 F. for an additional 2 hours. The mixture is reduced to ambient temperature and a solid polymer is recovered by filtration. The polymer is washed with water, partially air dried and dried for 12 hours at 250 F. The polymer, 25 grams, is then pyrolyzed at 300 to 450 F. in an air stream over a period of 12 hours. The material obtained is then pelleted and calcined at 800 F. for a period of 30 minutes under a nitrogen atmosphere. The polymer is then recovered. The polymer is then contacted with an aqueous solution of chloroplatinic acid under the conditions set forth above in Example 1. A platinum containing pyrolyzed polyacrylonitrile polymer is then recovered.

EXAMPLE 4 To a three-neck l-liter flask equipped with a stirrer, thermometer, and reflux condenser is added under a nitrogen atmosphere 55 grams (1.0 mole) of acrylonitrile, 7 grams of N/N'dimethylacrylamide, 750 milliliters of water and 1.0 gram of azobis-isobutyronitrile. The mixture is heated with stirring to a temperature of 140 F. which is maintained for a period of 2 hours. After this period 1 gram of azobisisobuperature and a solid polymer is recovered by filtration. The

I polymer is washed with water, partially air dried and dried for 12 hours at 250 F. The polymer 28 grams is then pyrolyzed at ing means and gas chromotography apparatus to determine the conversion to the desired product. The reactant inlet means consisted of a liquid receiver for holding the reactant and a gas bubbler which allowed hydrogen or helium gas to be solid polymer. is recovered by filtration. The polymer is washed with water, partially air dried and dried for 12 hours at 250 F. The polymer 40 grams is then pyrolyzed at 300 to 450 F. in an air stream over a period of 12 hours. The material obtained is then pelleted and calcined at 800 F. for a period of 30'minutes under a nitrogen atmosphere. The polymer is then recovered. The polymer is then contacted with an aqueous solution of chloroplatinic acid under the conditions set froth above in Example 1. A platinum containing pyrolyzed polyacrylonitrile polymer is then recovered.

In Tables I and II following are the results obtained for the hydrogenation-of 2-nitropropane to isopropylamine and the dehydrogenation of isopropyl alcohol to acetone. The apparatus that was utilized consisted of a 5 cc. micro-reactor equipped with reactant inlet means, product exit means, heat- 300 to 450 F. in an air stream over a period of 12 hours. The 5 bubbled through the reactant inlet means to the micro-reacmaterial obtained is then pelleted and calcined at 800 F. for a tor, For the hydrogenation of Z-nitropropane to period of 30 minutes under a nitrogen atmosphere. The isopropylamine, aspace velocity of 555 cubic centimeters per polymer is then recovered. The polymer is then contacted hour per gram of catalyst, a gas stream which comprised 1.84 with an aqueous solution of ehloroplatinic acid under the conmole percent 2-nitropropane and 98.2 percent mole hydrogen ditions setfroth above in Example 1. A platinum containing anda temperature of 250 F. were utilized. The analysis of the pyrolyzed polyacrylonitrile polymer is then recovered. rodu t wa done by gas chromatography. For the conversion of isopropyl alcohol to acetone, a space velocity of 555 cubic EXAMPLE 5 cc. per hour per gram of catalyst, a gas stream which com- To a three-neck l-liter flask equipped with a stirrer, therp f mole F P PY alcohol and -10 P mometer, and reflux condenser is added under a nitrogen atcent of helium and a temperature of 500 F. were utilized. The mosphere 60 grams .of acrylonitrile, 3 grams of products were analyzed by gas chromatography. The mole dimethylamaleate, 750 milliliters of water and 1.0 gram of percent conversion to the desired product and the mole perazo-bis-isobutyronitrile. The mixture is heated with stirring to cent of secondary products are set forth in Table I for the a temperature of 140 F. which is maintained for a period of 2 hydmgenatlon of f p fi to lsopl'opylamme n h Af hi i d 1 gram of bi i b i il i Table II for the conversion of isopropyl alcohol to acetone. ln added and the mixture stirred at 140 F. for an additional two Examples 8 and 13 9"? Tables I and fespectlvely, hours. The mixture is then reduced to ambient temperature the PY polyacrylomfnle P y was obtamed and a solid polymer is recovered by filtration. The polymer is p P to converslon of the P y to the Platmum washed with water, partially air dried and dried for 12 hours at Qm i y H TABLE I Iso- Dilso- Converpropyl propyl slon, amine, amine, Example mole mole mole Number Catalyst percent percent percent Comments 7 Girdler G659 a 100 Trace 38 44 mole percent trl-propylamine, 18

- mole percent n-propyl alcohol. Pyrolyzed polyacrylonitrile polymer N0 reaction.- 0.5 wt. percent Pt on silica gel l Nothing comes off catalyst. 10 Copper chromite 100 Trace 23 17 mole percent tri-propylamine, 24

, mole percent n-propyl alcohol. 11 0.5 wt. percent Pr on pyrolyzed polyacrylunltrile polymer from Ex. 1 100 99 12 5 wt. percent Ni on pyrolyzed polyacrylonitrile polymer from Ex. 2 100 96 3 I e 1'i i c lrel on kieselguhr with 2 wt. percent zirconium.

250 F. The polymer grains is then pyrolyzed at 300 to i TABLE II 450 F. in an air stream over a period of 12 hours. The material obtained is then pelleted and calcined at 800 F. for a period 15 of 30 minutes under a nitrogen atmosphere. The polymer is ogther then recovered. The polymer is. then contacted with an aque Prop!" than ver- Acelene, pylene, ous solution of chloroplatinic acid under the conditions set E 1 5101 1, tone, mole mole xam e 1 froth above ir Example A platinum containing pyrolyzed g, Catalyst gg z 135 gif gif polyacrylonitrile polymer is then recovered.

EXAMPLE 6 13 Pyrolyzed polyacryloni- To a three-neck l-liter flask equipped with a stirrer, ther- 14 %,,f;f{ sg 14 mometer, and reflux condenser is added a nitrogen atactivated carbon 100 4 96 15 0.75 wt. percent Pt on mosphere, grams (1.0 mole) of acrylonitrile, 4 grams of 1m gel 57 41 vinylacetate, 750 milliliters of water and 1.0 gram of azobi- 16 0flow-P910911: Pt on 55 pyrolyzed polyacrylosisobutyronitnle. The mixture is heated with stirring to a temnltrlle polymer from perature of F. which is maintained for a period of 2 1 98 95 20 hours. After this period 1 gram of azobisisobutyronitn'le is g a v added and the mixture stirred at 140 F. for an additional 2 hours. The mixture is reduced to ambient temperature and a 60 The results obtained set forth in Tables I and II demonstrate the outstanding performance of the process of this invention, for the conversion of organic nitro compounds to an organic primary amine, at high yields while minimizing the formation of undesired side reactions of products. More particularly, the results in Table I demonstrate that the Group VIII metal containing pyrolyzed polyacrylonitrile polymers produced 99 mole percent conversion of 2-nitropropane to isopropylamine in the case of platinum and 96 mole percent conversion in the case of nickel. These results are in sharp contrast to a copperchromite catalyst which produced trace quantities of isopropylamine and to the use of platinum on silica gel and to a pyrolyzed polyacrylonitrile polymer which produced essentially no reaction. With respect to theconversion of organic secondary alcohols to organic ketones, results in Table II demonstrate that the mole percent conversion utilizing the catalyst of this invention produced a conversion to acetone of 96 percent whereas a comparison with pyrolyzed polyacrylonitrile polymer platinum on activated carbon and platinum on silica gel, produced conversions to acetone of 2.6 percent, 4 percent, and 57 percent, respectively. Thus, in the cases of platinum catalysts other than the catalyst of this invention, conversions to undesired side reaction products was extensive. It is clear from the results set forth in Tables I and II that the catalyst of this invention produces high conversions to the desired product while minimizing the formation of undesired side reaction products. These results are in sharp contrast to those obtained with traditional platinum catalyst under the same'hydrogenation and dehydrogenation conditions.

We claim:

1. A dehydrogenation process which comprises reacting an organic secondary alcohol having the formula wherein R and R are hydrocarbon radicals containing from one to about 30 carbon atoms with a catalytic amount of a percent by weight polymerized monomer units derived from acrylonitrile.

3. A process of claim 1 wherein the catalyst is prepared from a polyacrylonitrile polymer which comprises at least percent by weight polymerized monomer units derived from acrylonitrile.

4. A process of claim 1 wherein the polyacrylonitrile polymer has a molecular weight of from about 25,000 to about 1,300,000.

5. A process of claim 1 wherein the organic secondary alcohol is isopropyl alcohol, and the organic ketone is acetone.

6. A process of claim 2 wherein the organic secondary alcohol is isopropyl alcohol, and the organic ketone is acetone.

7. A process of claim 4 wherein the organic secondary alcohol is isopropyl alcohol, and the organic ketone is acetone. 

2. A process of claim 1 wherein the catalyst is prepared from a polyacrylonitrile polymer which comprises at least 90 percent by weight polymerized monomer units derived from acrylonitrile.
 3. A process of claim 1 wherein the catalyst is prepared from a polyacrylonitrile polymer which comprises at least 95 percent by weight polymerized monomer units derived from acrylonitrile.
 4. A process of claim 1 wherein the polyacrylonitrile polymer has a molecular weight of from about 25,000 to about 1,300,000.
 5. A process of claim 1 wherein the organic secondary alcohol is isopropyl alcohol, and the organic ketone is acetone.
 6. A process of claim 2 wherein the organic secondary alcohol is isopropyl alcohol, and the organic ketone is acetone.
 7. A process of claim 4 wherein the organic secondary alcohol is isopropyl alcohol, and the organic ketone is acetone. 